Patent GB-606664-A (GB)
Title: Improved process for the catalytic hydroforming of naphthas
IPC: C10G35/14
Filed: 1945-04-26
Abstract: <PICT:0606664/III/1> In hydroforming naphthas by contacting the vapours with a fluidized hydroforming catalyst, contaminated catalyst being continuously withdrawn, regenerated with an oxygen-containing gas and recycled, the catalyst comprises a Group 6 metal oxide, and an alkaline earth metal oxide on a zinc spinel base.  Oxides of Mo, Cr, and W stabilized with oxides of Ca, Mg, Sr, and Ba are specified. A suitable molar ratio of Mo to Ca is 1 : 1.  The spinel should comprise 50-95 per cent by weight of the catalyst. The catalyst may be prepared as described in Specification 605,868 by adding acidified zinc nitrate, and alkaline sodium aluminate solutions to water, and calcining the washed precipitate at 1000 DEG  F.  This is stirred in calcium nitrate solution, filtered, ignited to decompose the nitrate, mixed with ammonium molybdate solution, dried, pilled, and calcined at 1200 DEG  F.  The hydroforming of a 200-240 DEG  F. naphthenic naphtha to give toluene, using a fluidized catalyst of molybdenum oxide 10 per cent, calcium oxide 4 per cent, and zinc spinel 86 per cent, of particle size up to 100m , is described.  Reaction conditions for the reforming may be 850-1050 DEG  F., 0-500 p.s.i., with a residence time of catalyst 0.25-60 mins., and for the regeneration 1000-1400 DEG  F. at similar pressure and 0.5-15 mins. The naphtha and hydrogen, separately preheated, enter the lower bend of standpipe 3 by line 30 to mix with the catalyst which flows from hopper 1 and is fluidized by gas injected through taps 5.  Vapours leaving the reactor 35 pass by line 42 to recovery apparatus while catalyst is withdrawn through pipe 39, fluidized in an oxygen containing gas, and passed to regenerator 60, regenerated catalyst being returned by pipe 100 to hopper 1.ALSO:<PICT:0606664/IV(b)/1> In hydroforming naphthas by contacting the vapours with a fluidized hydroforming catalyst, contaminated catalyst being continuously withdrawn, regenerated with an oxygen-containing gas and recycled, the catalyst comprises a Group 6 metal oxide, and an alkaline earth metal oxide on a zinc spinel base.  Oxides of Mo, Cr, and W stabilized with oxides of Ca, Mg, Sr, and Ba are specified.  A suitable molar ratio of Mo to Ca is 1 : 1.  The spinel should comprise 50-95 per cent by weight of the catalyst. The catalyst may be prepared as described in Specification 605,868, [Group III], by adding acidified zinc nitrate, and alkaline sodium aluminate solutions to water, and calcining the washed precipitate at 1000 DEG F.  This is stirred in calcium nitrate solution, filtered, ignited to decompose the nitrate, mixed with ammonium molybdate solution, dried, pilled, and calcined at 1200 DEG  F.  The hydroforming of a 200-240 DEG  F. naphthenic naphtha to give toluene, using a fluidizedcatalyst of molybdenum oxide 10 per cent, calcium oxide 4 per cent, and zinc spinel 86 per cent, of particle size up to 100m , is described. Reaction conditions for the reforming may be 850-1050 DEG  F., 0-500 p.s.i., with a residence time of catalyst 0.25-60 mins., and for the regeneration 1000-1400 DEG  F. at similar pressure and 0.5-15 mins. The naphtha and hydrogen, separately preheated, enter the lower bend of standpipe 3 by line 30 to mix with the catalyst which flows from hopper 1 and is fluidized by gas injected through taps 5.  Vapours leaving the reactor 35 pass by line 42 to recovery apparatus while catalyst is with drawn through pipe 39, fluidized p  in an oxygen-containing gas, and passed to regenerator 60, regenerated catalyst being returned by pipe 100 to hopper 1.